Para-selective alkylation catalysts and processes

Description

[0001] This invention relates to preparation of improved zeolite-based catalysts especially useful for promoting the alkylation of mono-alkyl aromatic compounds to form a dialkyl substituted aromatic product enriched in the para (i.e., 1,4-)dialkyl benzene isomer. The invention also relates to a process for the alkylation, e.g., ethylation, of monoalkyl aromatic compounds, e.g. toluene or ethylbenzene, in a manner so as to maximize the production of the product para-isomer, to minimize the production of the product meta isomer and to substantially eliminate the production of the product ortho isomer.

[0002] Zeolite-containing compositions are well known catalysts for promoting conversion of aromatic hydrocarbons to dialkyl substituted aromatic compounds via alkylation, transalkylation, disproportionation and isomerization reactions. Numerous techniques are also known for modifying zeolite-based aromatics conversion catalysts of this type in order to provide catalysts which promote production of a reaction product which is enriched in the para-isomer of the desired disubstituted aromatic material. For example, Kaeding, U.S. Patent 4,117,024, Issued September 26, 1978 and assigned to Mobil Oil Corporation, discloses a process for the conversion of toluene and/or ethyl benzene to its corresponding para ethyl alkylation product by carrying out the alkylation in the presence of hydrogen and using as a catalyst a crystalline aluminosilicate zeolite of specified acidity, sorption characteristics and Constraint Index. This U.S. Patent 4,117,024 discloses many materials which exemplify this genus of catalysts including, but not limited to, ZSM-5, ZSM-11, ZSM-12, ZSM-35, and ZSM-38. U.S. Patent 4,117,024 also discloses that the zeolite material may be modified in one or more ways to improve the para-selectivity properties of the catalyst. Several additional U.S. Patents including U.S. Patent 4,034,053, U.S. Patent 4,049,573 and U.S. Patent 4,086,287, represent additional applicable prior art involving the modification of zeolite based catalysts of this same general type in order to improve the para-selectivity characteristics thereof when such materials are used to promote various aromatic hydrocarbon conversion reactions, including alkylation of monoalkyl substituted aromatics to produce dialkylbenzene compounds.

[0003] In addition, EP-A-14545 discloses a method of preparing a para-selective catalyst for use in, for example, the alkylation of toluene, by impregnating and/or ion-exchanging a zeolite having a silica to alumina ratio of at least 12 and a Constraint Index of 1 to 12 with a Groupe IIA metal salt, for example, magnesium nitrate, or a Group VIII metal salt and then calcining the resultant product.

[0004] Considering all of such prior art references together, a process has been designed for the commercial production of para-ethyltoluene by the catalytic ethylation of toluene with ethylene using cofed hydrogen. Such a process utilizes what was heretofore believed to be the best catalyst for maximizing para-isomer, minimizing metal-isomer, eliminating ortho isomer, providing high conversion of reactants to products and permitting low catalyst aging rate. This optimized prior art catalyst is a crystalline siliceous material of ZSM-5 topology, as characterized by significant x-ray diffraction pattern lines, which is composited with a binder and is then impregnated with both phosphorus and magnesium. This selected catalyst is made by a series of process steps comprising: preparing the siliceous crystalline zeolite; binding the zeolite with a matrix material, suitably alumina; steaming the resulting zeolite-containing composite; impregnating the composite with diammonium phosphate followed by filtering, drying and calcining the resulting phosphorus-impregnated composite; contacting the P-containing composite in a first magnesium impregnation stage with a magnesium acetate solution, followed by calcination; thereafter contacting the composite, in a second separate magnesium impregnation stage, with another batch of magnesium acetate solution, followed again by calcination to prepare the final form catalyst. The modified zeolite catalyst produced in this manner is well suited to use in the toluene ethylation process. As can be seen from the data presented in U.S. Patent 4,117,024, an ethyl toluene product is thus produced having desirable isomeric distribution characteristics, with very advantageous catalyst life and conversion capability.

[0005] From the foregoing preparation description and referenced data, it can be seen that the prior art catalyst selected as the best for commercialization, i.e. a magnesium and phosphorus impregnated, alumina-bound zeolite material, achieves its best selectivity for ethylene alkylation of toluene to para-ethyltoluene at impregnant loadings of 7 and 3 weight percent respectively for magnesium and phosphorus, provided the catalyst composite into which these materials are impregnated is presteamed. Without wishing to be bound by theory, it is believed that the magnesium being impregnated onto such a catalyst can have a significant affinity for the binder portion of the catalyst composite. It if further believed that the initial treatment of the prior art catalyst composite with the phosphorus impregnant serves to "passivate" the binder material, thereby promoting greater association of magnesium with the zeolite portion of the composite upon subsequent treatment of the composite with the magnesium acetate solution. Since it is expected that it is magnesium associated with the zeolite material in such composite which provides the excellent selectivity characteristics of such prior art composites for production of para-ethyltoluene, the phosphorus followed by magnesium treatment of such composites serves to provide highly desirable toluene alkylation catalysts.

[0006] Notwithstanding the suitability of such prior art MG-P-ZSM-5 type zeolite catalyst composites for use in the commercial-scale production of para-ethyltoluene, there are still several disadvantages associated with the large scale preparation of catalysts of this type in the manner described. For example, if the impregnated catalyst is not presteamed, para-ethyltoluene selectively may not be as high as needed for some commercial production operations. Furthermore, magnesium impregnation concentration to the optimum 7 weight percent cannot generally be achieved during commercial scale catalyst production, when using a magnesium acetate impregnant solution, in a single impregnation. Multiple impregnations, with intermediate calcination, are usually required during commercial scale production to achieve the requisite 7% concentration of magnesium. Still further, even to achieve this result using multiple impregnations, it is necessary to use very concentrated aqueous magnesium acetate solutions, e.g. about 50 to 60 weight percent in water. Such solutions are very viscous and thus have to be utilized as impregnants at elevated temperatures, e.g. about 150°F, in order to reduce impregnant viscosity to acceptable impregnation levels.

[0007] All of the foregoing recited disadvantages of the previously selected optimum magnesium/phosphorus based alkylation catalyst composites should not be taken to in any way mean that such a catalyst was or is unsatisfactory. Quite to the contrary, such a prior catalyst is excellent, far superior to it predecessors and is quite well suited to use in the aromatics alkylation processes described. It is furthermore commercially manufacturable, albeit with some difficulty and expense. Notwithstanding the suitability of such prior art alkylation catalysts, there is nevertheless a continuing need to develop additional catalysts, catalyst preparation procedures and alkylation processes employing such catalysts which provide one or more performance or commercial advantages over similar catalysts, procedures and processes of the prior art.

[0008] Accordingly, it is an object of the present invention to provide an additional type of zeolite-based catalyst composition suitable for promoting the para-selective conversion of monoalkyl aromatics such as toluene to dialkylbenzene materials such as para-ethyltoluene. It is a further object of the present invention to provide such an additional type of alkylation catalyst which is substantially phosphorus-free but which nevertheless exhibits selectivity and activity characteristics comparable or superior to those of the hereinbefore described magnesium phosphorus alkylation catalysts of the prior art. It is further an object of the present invention to provide such an additional type of alkylation catalyst which, in comparison with preferred prior art catalysts is simpler and easier to manufacture via a novel method for catalyst preparation. It is a further object of the present invention to provide an aromatics alkylation process employing such an improved zeolite-based alkylation catalyst.

[0009] The present invention relates primarily to a method for preparing a novel improved phosphorus-free aromatics alkylation catalyst. This catalyst preparation method involves the essential steps of preparing a zeolite-containing base catalyst composite, contacting this base catalyst composite, preferably in a single stage operation, with an aqueous solution of a single selected impregnating compound, magnesium nitrate, and thereafter calcining the magnesium nitrate treated catalyst composite to form the desired aromatics alkylation catalyst.

[0010] The zeolite material used to form the base catalyst composite is siliceous crystalline zeolite having a silica to alumina molar ratio of at least about 12, a Constraint Index within the approximate range of 1 to 12 and a zeolite crystal having a major dimension of from about 1 to 10 micrometers and a minor dimension of from about 0.2 to 4 micrometers. Such materials are exemplified by the zeolites ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, and ZSM-48. The zeolite material is-combined with an inorganic oxide binder (i.e., matrix) material to form a catalyst composite comprising from about 1 to 99% by weight of the zeolite and from about 1 to 99% by weight of the binder.

[0011] The magnesium nitrate treating step is conducted under conditions and for a length of time suitable to incorporate magnesium nitrate with the base catalyst composite in an amount which provides from about 4% to 8% by weight of magnesium on the resulting alkylation catalyst upon subsequent calcination of the treated composite. Since magnesium nitrate is the only catalyst modifier utilized, there need be no contact of the catalyst composite with any solutions of phosphorus compounds, and the resulting catalyst is therefore substantially phosphorus free.

[0012] The calcination step which renders the catalyst ready for use is carried out in a nitrogen or oxygen-containing atmosphere at a temperature of from about 200°C to 565°C. Such calcination is conducted for a time sufficient to provide a ready-to-use alkylation catalyst that contains from about 4% to 8% by weight of magnesium which is present in the catalyst at least in part as magnesium oxide.

[0013] In its composition aspects, the present invention relates to the aromatics alkylation catalyst composition prepared in accordance with the catalyst preparation method hereinbefore described. Also claimed is the modified base catalyst composite which consists essentially of zeolite, inorganic oxide binder and magnesium nitrate and which is prepared in accordance with the first two steps of the catalyst preparation method hereinbefore described.

[0014] Finally in its process aspects, the present invention relates to an aromatics alkylation process utilizing the magnesium oxide impregnated, substantially phosphorus-free catalyst compositions hereinbefore described. Such compositions can be suitably employed to promote alkylation (e.g., ethylation) of mono- alkyl aromatics such as toluene to produce a dialkylbenzene product mixture enriched in the para-dialkyl- isomer, e.g. ethyltoluene mixtures enriched in para-ethyltoluene.

[0015] In accordance with the present invention, base catalyst composites comprising a particular type of zeolite material are modified to provide catalysts which are especially useful for promoting para-selective alkylation of monoalkyl benzene compounds. The siliceous crystalline zeolites used in such base catalyst composites are members of a special class of zeolites that exhibits unusual properties. Such zeolite materials are those which have a silica to alumina molar ratio of at least 12 and a constraint index within the range of 1 to 12. Zeolite matrials of this type are well known. Such zeolites and their use as catalysts for alkylation of aromatic hydrocarbons are generally described, for example, in U.S. Patent No. 4,302,622. Crystalline zeolites of the type useful in the catalysts of the present invention include ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38 and ZSM-48, with ZSM-5 being particularly preferred.

ZSM-5 is described in greater detail in U.S. Patent Nos., 3,702,886 and Re 29,948, which patents provide the X-ray diffraction pattern of the therein disclosed ZSM-5.

ZSM-11 is described in U.S. Patent No. 3,709,979, which discloses in particular the X-ray diffraction pattern of ZSM-12.

ZSM-12 is described in U.S. Patent No. 3,832,449, which discloses in particular the X-ray diffraction pattern of ZSM-12.

ZSM-23 is described in U.S. Patent No. 4,076,842, which discloses in particular the X-ray diffraction pattern of ZSM-23.

ZSM-35 is described in U.S. Patent No. 4,016,245, which discloses in particular the X-ray diffraction pattern of ZSM-35.

ZSM-38 is described in U.S. Patent No. 4,046,859, which discloses in particular the X-ray diffraction pattern of ZSM-38..

ZSM-48 is more particularly described in European Patent Publication EP-A-0015132 which includes the X-ray diffraction pattern for ZSM-48.

[0016] The size of the zeolite crystals employed in the alkylation catalyst composites of this invention can also affect the selective catalytic properties of such a catalyst. For highest selectivity to para-isomer alkylation, it is preferred that the size of the zeolite crystals utilized range from about 1 to 10 pm, more preferably from about 2 to 4 µm along the major dimension (crystal length) and from about 0.2 to 4 µm, more preferably about 0.5 to 2 µm along the minor dimension (crystal thickness).

[0017] When synthesized in the alkali metal form, the zeolite used to form the base catalyst composite can be conveniently converted in a conventional manner to the hydrogen form, generally by intermediate formation of the ammonium form as a result of ammonium ion exchange and calcination of the ammonium form to yield the hydrogen form of the zeolite. In addition to the hydrogen form, otherforms of the zeolite can be employed in the base catalyst composition so long as the original alkali metal has been reduced to less than about 50% by weight of the original alkali metal contained in the zeolite as- synthesized, preferably 0.5% by weight of less. Thus, the original alkali metal of the zeolite may be replaced by ion exchange with other suitable metal cations of Groups I through VIII of the Periodic Table, including, by way of example, nickel, copper, zinc, palladium, calcium or rare earth metals.

[0018] In preparing the zeolite-containing base catalyst composites of the present invention, the above-described siliceous crystalline zeolite material is combined with an inorganic oxide binder or matrix comprising another material resistant to the temperature and other conditions employed in the process for preparing the modified catalyst composites and compositions of the present invention and/or in the subsequent aromatics alkylation process embodiments in which the resulting alkylation catalyst compositions are employed. Such matrix material is useful as a binder and imparts greater resistance to the catalyst for the severe temperature, pressure and reactant feed stream velocity conditions encountered in such processes.

[0019] Useful matrix materials include both synthetic and naturally occurring substances, as well as inorganic materials such as clay, silica and/or metal oxides. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Naturally occurring clays which can be composited with the zeolite include those of the montmorillonite and kaolin families, which families include the sub-benonites and the kaolins commonly known as Dixie, McNamee-Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite or anauxite. Such clays can be used in the raw state or originally mined or initially subjected to calcination, acid treatment or chemical modification.

[0020] In addition to the foregoing materials, the binder for the siliceous crystalline zeolite material employed herein can comprise a porous matrix material, such as alumina, silica-alumina, silica-magnesia, silica- zirconia, silica-thoria, silica-beryllia, and silica-titania, as well as ternary compositions, such as silica- alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia. The matrix may be in the form of a cogel. The relative proportions of zeolite component and inorganic oxide gel matrix, on an anhydrous basis, may vary widely with the zeolite content ranging from between about 1 to about 99 percent by weight and more usually in the range of about 25 to about 80 percent by weight of the dry base composite.

[0021] In prior art processes for modifying base catalyst composites of the type hereinbefore described, such base catalyst composites of this type are frequently subjected at this point in catalyst preparation to a pre-steaming procedure as one step in the process of preparing para-selective aromatics alkylation catalysts. Such pre-steaming treatment serves to enhance the para-selectivity characteristics of the alkylation catalyst eventually prepared. It has been discovered that by employing the particular base catalyst composite treatment procedure hereinafter described, such a pre-steaming step can be eliminated and yet the para-selectivity of the resulting alkylation catalyst will be as good as or better than that of a steam selectivated Mg-P impregnated catalyst of the prior art.

[0022] Thus, as a second step in the catalyst preparation process of the present invention, the base catalyst composites prepared as hereinbefore described can be contacted with an aqueous solution of the particular selected catalyst modifying agent magnesium nitrate. Such contact of base catalyst composites with magnesium nitrate solution generally occurs under treatment conditions which are, and for a time period which is, sufficient to incorporate magensium nitrate with the composite in an amount which will provide from about 4% to 8% by weight of magnesium on the aromatics alkylation catalysts which eventually are formed upon subsequent calcination of the modified base catalyst composites. Such amounts can comprise, for example, from about 25% to 50%, more preferably from about 30% to 45%, by weight of magnesium nitrate on the base catalyst composite on an anhydrous basis.

[0023] The aqueous solution of magnesium nitrate used in this contacting step can be prepared by simply dissolving an appropriate form of magnesium nitrate, e.g., (Mg(N0₃)₂.2H₂0 or Mg(NO₃)₂.6H₂O, with water to form the treating solution for the base catalyst composites. If desired, inert cosolvents such as lower alkanols can be employed in forming this magnesium nitrate solution. Magnesium nitrate concentrations of from about 40% to 65%, more preferably from about 60% to 65%, by weight of solution can advantageously be employed in forming the magnesium nitrate composite treating solution.

[0024] Contact between base catalyst composites and magnesium nitrate solution can be effected by any suitable means conventionally used to treat solid particulate material with a treating agent in liquid form. Such techniques can, for example, involve soaking the base catalyst composites in the magnesium nitrate solution in a suitable vessel or may involve continuous or intermittent contact of the magnesium nitrate solution with a bed of catalyst composite particles. The ebullated bed arrangement of U.S. Patent No. 4,292,205 represents another useful means for effecting catalyst contact with the magensium nitrate treating solution.

[0025] No matter what particular contact arrangement may be employed, the handling of the magnesium nitrate solution in such procedures is generally much easier than the handling of the impregnating solutions in corresponding prior art procedures which utilize comparatively much more viscous solutions of magnesium acetate. The viscous behavior of concentrated magnesium acetate solutions can make catalyst impregnation difficult in such prior art processes since channeling and catalyst flotation may become problems in larger vessels used for impregnation. Catalyst treatment using magnesium nitrate solutions, on the other hand, can be accomplished with fewer processing and equipment difficulties in comparison with magnesium acetate impregnation. It is furthermore apparent that since the magnesium nitrate treated catalyst composites are not to be phosphorus-modified, the composites of the present invention are not therefore contacted with solutions of phosphorus compounds either prior to or subsequent to their treatment with the magnesium nitrate solution.

[0026] The efficiency of commercial scale catalyst composite impregnation is also significantly improved with magnesium nitrate impregnation in comparison with impregnation using aqueous magnesium acetate solution. Using magnesium nitrate solutions, it is in fact possible to incorporate the requisite amount of magnesium onto the catalyst composite in a single impregnation stage without intermediate drying or calcination, provided the impregnated catalyst material is dried by free convection methods. Even when forced convection gas is used to dry the impregnated composites (thereby blowing some of the impregnating solution off the catalyst material), it is possible to reach optimum magnesium content using a magnesium nitrate impregnant in as few as two impregnation stages.

[0027] As noted, contact between magnesium nitrate treating solution and the base catalyst composite occurs for a time period which is sufficient to effect incorporation of the requisite amount of magnesium nitrate onto the base catalyst composites. Contact times of at least about 0.5 hour, more preferably from about 1 to 2 hours, may advantageously be utilized. Contacting conditions will generally also include a contact temperature from about 10°C to 65°C, more preferably from about 20°C to 55°C.

[0028] After contact of the catalyst composites with magnesium nitrate solution is completed to the extent desired, the treated catalyst composites can thereafter be dried and calcined to form the finished catalyst compositions suitable for use in promoting para-selective alkylation reactions. Calcination will generally occur in a nitrogen and/or oxygen-containing atmosphere, e.g. air, which may also contain diluents such as helium and the like. Calcination can be carried out at a temperature of from about 200°C to 565°C, more preferably from about 510°C to 540°C, and for a time sufficient to provide a modified catalyst composition containing from about 4% to 8%, more preferably from about 6% to 7%, by weight of magnesium on the finished catalyst composition. At least some of the magnesium present in the calcined catalyst composition is thus present in the form of magnesium oxide. Calcination under such conditions can thus advantageously be carried out for a period of from about 1 to 6 hours, more preferably from about 2 to 6 hours.

[0029] The magnesium nitrate treated zeolite catalysts of the present invention can be advantageously used to promote conversion of mono-alkyl aromatic compounds to provide dialkyl substituted benzene product mixtures which are highly enriched in the para-dialkyl substituted benzene isomer. Conversion reactions of this type thus involve an aromatics alkylation reaction. Alkylation of aromatic compounds in the presence of the above-described catalysts can be effected by contact of the aromatic with an alkylating agent under alkylation conditions. A particularly preferred embodiment involves the alkylation of toluene wherein the alkylating agents employed comprise methanol or other well known methylating agents or ethylene. The reaction is carried out at a temperature of between about 350°C and about 750°C, preferably between about 300°C and 650°C. At higher temperatures, the zeolites of high silica/alumina ratio are preferred. For example, ZSM-5 having a SiO₂/AI₂O₃ ratio of 30 and upwards is exceptionally stable at high temperatures. The reaction generally takes place at atmospheric pressure, but pressures within the approximate range of 10⁵ N/m² to 10' N/m² (1-100 atmospheres) may be employed.

[0030] Some non-limiting examples of suitable alkylating agents would include olefins such as, for example, ethylene, propylene, butene, decene and dodecene, as well as formaldehyde, alkyl halides and alcohols, the alkyl portion thereof having from 1 to 16 carbon atoms. Numerous other aliphatic compounds having at least one reactive alkyl radical may be utilized as alkylating agents.

[0031] Aromatic compounds which may be selectively alkylated as described herein would include an alkylatable mono-alkyl aromatic hydrocarbon such as, for example, ethylbenzene, toulene, propylbenzene, isopropylbenzene, or substantially any mono-substituted benzenes which are alkylatable in the 4-position of the aromatic ring.

[0032] The molar ratio of alkylating agent to aromatic compound is generally between about 0.05 and about 2. For instance, when methanol is employed as the methylating agent and toluene is the aromatic, a suitable molar ratio of methanol to toulene has been found to be approximately 0.1 to 1.0 mole of methanol per mole of toluene. When ethylene is employed a the alkylating agent and toluene is the aromatic, a suitable molar ratio of ethylene to toluene is approximately 0.05 to 2.5 moles of ethylene per mole of toluene.

[0033] Alkylation is suitably accomplished utilizing a feed weight hourly spaced velocity (WHSV) of between about 1 and about 100, and preferably between about 1 and about 50. The reaction product, consisting predominantly of the 1,4-dialkyl isomer, e.g. 1,4-dimethylbenzene, 1-ethyl-4-methylbenze, etc., or a mixture of the 1,4- and 1,3-isomer, may be separated by any suitable means. Such means may include, for example, passing the reaction product stream through a water condenser and subsequently passing the organic phase through a column in which chromatographic separation of the aromatic isomers is accomplished. Alkylation using the magnesium nitrate-treated catalysts of the present invention can provide product mixtures containing at least 80% or even 90% or more by weight of the para-dialkylbenzene isomer.

[0034] The aromatic alkylation process described herein may be carried out as batch type, semi-continuous or continuous operations utilizing a fixed or moving bed catalyst system. The catalyst after use in a moving bed reactor can be conducted to a regeneration zone wherein coke is burned from the catalyst in an oxygen-containing atmosphere, e.g. air, at an elevated temperature, after which the regenerated catalyst can be recycled to the alkylation zone for further contact with the charge stock. In a fixed bed reactor, regeneration can be carried out in a conventional manner where an inert gas containing a small amount of oxygen (0.5-2%) is used to burn the coke in a controlled manner so as to limit the temperature to a maximum of around 500°-550°C.

[0035] Siliceous zeolite crystal-containing composites treated with magnesium nitrate according to this invention show remarkably better catalytic properities for the alkylation of monoalkylbenzene than do corresponding composites impregnated with magnesium acetate to the same magnesium content. It is recognized that the aforementioned U.S. Patent 4,117,024 describeds and claims siliceous crystals impregnated with one or more of phosphorous, boron, antimony or magnesium and that this patent describes a host of magnesium introducing impregnants including inter alia magnesium acetate and magnesium nitrate. It is also recognized that this U.S. Patent 4,117,024 describes and prefers the use of relatively large crystals (about 1 to 5 µm) of siliceous zeolite materials. However, U.S. Patent 4,117,024 does not recognize that zeolite crystal-containing composites impregnated with magnesium nitrate are not equivalent to such composites impregnated with other magenisum salts, notably magnesium acetate, for the alkylation, e.g., ethylation, of mono substituted, particularly alkylated, most particularly methyl, benzenes to produce the desired product distribution described above in an optimal fashion. The particular magnesium-containing catalyst compositions of the present invention which have been prepared using a magnesium nitrate impregnant in fact represent catalysts which provide improved conversion of mono- alkylaromatics to dialkylaromatics, with improved selectivity of such conversion to production of para-dialkyl aromatic isomers and with reduced off-stream for catalyst regeneration and re-selectivation.

[0036] Without being bound to any particular theory of invention operability, it is speculated that the catalyst performance benefits achieved with the magnesium nitrate impregnated catalyst composite result from the enhanced tendency of magnesium nitrate solutions to deliver magnesium to the siliceous zeolite crystal portion of the catalyst composite versus the binder portion of the composite. It is perhaps this enhanced incorporation of magnesium from Mg(N0₃) into the siliceous zeolite crystalline material which permits elimination of the binder passivating phosphorus treatment step which is necessary to produce composites of desirably high para-selectivity when a magnesium acetate impregnant is employed.

[0037] The following examples will serve to illustrate certain specific emobidments of the hereindisclosed invention. These examples should not, however, be construed as limiting the scope of the invention, as there are many variations which may be made thereon without departing from the spirit of the disclosed invention, as those of skill in the art will recognize.

Example I

Part A - Converting Extrudate to Ammonium Form

[0038] Untreated base catalyst composites utilized are in the form of 4.2 mm (1/6") extrudate containing 65% by weight of ZSM-5 and 35% by weight alumina binder. ZSM-5 crystal size in such composites is approximately 1 pm in length, 0.5pm in thickness. Six pounds (2728 g; 4200 cm³) of this dried extrudate are charged to an ion exchange/calcination vessel. Extrudate therein is precalcined in N² at 540°C for 3 hours at a flow rate of 0.035 m³/minute (1.25 SCFM).

[0039] After cooling, the extrudate is ion exchanged with 19 kg (42 pounds) of 1 N ammonium nitrate solution at room temperature for one hour. After draing, the procedure is repeated and followed by 5 volumetric washes with deionized water. (Each is one complete fill followed by draining).

[0040] The extrudate is then dried in warm flowing N₂ and sampled. Sodium content is less than 0.01 wt.%. The zeolite portion of the extrudate is now in the ammonium form with the extrudate having the following composition:

Part B - First Magnesium Impregnation

[0041] Twelve kilograms of 60% weight (Mg(N0₃)2.6H₂0 are prepared. This solution is introduced to the ammonium form extrudate still in place in the ion exchange/calcination vessel. The solution is pumped upflow in a recycle mode for 5 minutes, then allowed to stand for one hour, all at room temperature. Before draining, the solution is again circulated for 5 minutes at 650 cm³/min. Solution is then drained and the extrudate dried in warm N₂ at a flow of 0.016 m³/minute (0.55 SCFM) (Standard Cubic Feet Per Minute).

[0042] After all points in the bed registered greater than 120°C (250°F), the extrudate is considered completely dry. Gas flow rate is increased to 0.035 m³/minute (1.25 SCFM) and temperatures increased to effect calcination. When bed temperatures are approximately 425°C (800°F), gas composition is changed to air, and the temperature increased to approximately 540°C (1000°F) and held for 2 hours. The bed is then cooled in N₂ and sampled.

[0043] The sample is found to have 3.8 wt.% Mg and an alpha activity of 51.

Part C - Second Magnesium Impregnation

[0044] 7.9 Kg of magnesium nitrate solution recovered from the first impregnation is supplemented with 2.1 Kg of fresh 60% Mg(N0₃)₂.6H₂0 to effect a second impregnation of the extrudate still in the vessel. The procedure is exactly as described for the first impregnation, including draining, drying and calcination. After cooling, the contents of the vessel are discharged. The finished catalyst is characterized as follows:

Example II

[0045] A large scale batch of ammonium form extrudate is prepared as described in Part A of Example I. A sample of this extrudate (800 cm³) is steamed in laboratory steamers (400 _CM³ each) in 100% steam, at one atmosphere and 540°C (1000°F) for 5 hours.

[0046] A sample of the steamed extrudate (100 cm³) is impregnated in a beaker with 200 cm³ of a 66 wt.% solution of Mg(N0₃)₂.6H₂0 for one hour at room temperature, with occasional stirring. The extrudate is drained on a screen, placed in a porcelain evaporating dish which is placed in a laboratroy drier kept at 120°C (250°F), and allowed to dry over a weekend.

[0047] The dried impregnated extrudate is then placed in a one pint muffle pot (a device to hold catalyst and allow positive gas flow from outside a muffle furnace) and is heated in 300 cm³/min of N₂ to a temperature of about 425°C (800°F). At this point N₂ is replaced by air and the temperature of the impregnated extrudate is increased to 540°C (1000°F) and held for two hours. The sample is cooled down in N₂.

[0048] Such a catalyst sample has a magnesium content of 7.0% by weight.

Example III

[0049] The procedure of Example II is repeated with a separate sample of ammonium form ZSM-5 extrudate. In this procedure, however, the concentration of the impregnating solution is 60% by weight Mg(N0₃)₂.6H₂0.

[0050] Such a catalyst sample has a magnesium content of 6.4% by weight.

Example IV

[0051] A 50 cm³ sample of the ammonium form ZSM-5 extrudate of Example I is calcined in N₂ for 3 hours at 540°C (1000°F). The cooled sample is then impregnated at 55°C (130°F) with 100 cm³ of a 60% Mg(OAc)₂.4H₂0 solution for 2 hours. The sample is drained, dried and calcined as described in Example II.

[0052] Such a catalyst sample has a magnesium content of 7.3% by weight.

Example V

[0053] A 100 cm³ sample of the ammonium form ZSM-5 extrudate of Example I is calcined in N₂ for 3 hours at 540°C (1000°F). The sample is cooled and impregnated with 60% Mg(NO₃)₂.6H₂O (200 cm³) for one hour at room temperature. The sample is then drained, dried and calcined as described in Example II.

[0054] Such a catalyst sample has a magnesium content of 6.9% by weight.

Example VI

[0055] A 100 cm³ sample of another batch of ammonium form ZSM-5 extrudate prepared in a manner substantially similar to that of Example I is impregnated with Mg using 200 cm³ of a 60% solution of Mg(NO₃)₂.6H₂O for one hour at 55°C (130°F). The sample is then drained, dried and calcined as described in

Example II.

[0056] Such a catalyst sample has a magnesium content of 6.8% by weight.

Example VII

[0057] A 50 cm³ sample of the same batch of ammonium form ZSM-5 extrudate of Example VI is impregnated using 100 cm³ of 55% Mg(NO₃)₂.6H₂O solution for one hour at room temperature (approximately 24°C/75°F). The sample is then drained, dried and calcined as described in Example II.

[0058] Such a catalyst sample has a magnesium content of 6.2% by weight.

Example VIII

[0059] The procedure of Example VII is repeated with a separate sample of the same ammonium form ZSM-5 extrudate. In this procedure, however, the concentration of the impregnating solution is 50% by weight of Mg(NO₃)₂.6H₂O.

[0060] Such a catalyst sample has a magnesium content of 5.4% by weight.

Example IX

[0061] A 50 cm³ sample of the ammonium form ZSM-5 extrudate from the ion exchange/calcination vessel of Example I is impregnated with 100 cm³ of 60% Mg(N0₃)₂.6H₂0 for one our at room temperature (approximately 24°C/75°F).

[0062] Such a catalyst sample has a magnesium content of 7.3% by weight.

Example X

[0063] Approximately 2180 kg (4,800 lbs) of untreated ZSM-5 base catalyst composites of the type described in Example I, Part A, are charged to an ion exchange/calcination vessel. The bed of extrudate in the vessel is heated in N₂ to 540°C (1000°F) and held for 3 hours (18.1 m³/minute [640 SCFM] of N₂). After cooling in N₂, the bed is ion-exchanged with a solution made up from 272 kg (600 lbs) of ammonium nitrate and 9577 I (2,530 gallons) of deionized water for 3 hours at ambient temperature with a circulation of 379 I (100 gallons) per minute. After draining and washing with 9464 I (2,500 gallons) of deionized water, the procedure is repeated. A sample from the bed, after drying analyzes at 0.01 wt.% Na.

[0064] The bed is dried, unloaded and split in half. One half, i.e. 1086 kg (2,393 lbs), are reloaded into the vessel. The bed is impregnated with a 60% weight solution of Mg(N0₃)₂.6H₂0 made by dissolving 4767 kg (10,500 lbs) of Mg(NO₃)₂.6H₂O in 31762 (839 gallons) of deionized water. After the bed is completely wetted, solution is circulated for 15 minutes at 2461 I (650 gallons) per minute. Solution is allowed to stand for one hour and is then recirculated again for 15 minutes. Solution is then drained by pumping solution back to the original solution tank.

[0065] The treated extrudate is then dried by flow of air (3.7 m³/minute [130 SCFM]) at 232°C (450°F) leaving the furnace. After 48 hours, the bed is considered completely dry (all temperatures above 163°C [325°F]), and flow is switched to N₂ and increased to 20.4m³/minute (720 SCFM) for calcination. The furnace temperature is increased, and at an average bed temperature of 427°C (800°F), the furnace is held constant for 2 hours. N₂ is then replaced with air, and the furnace temperature is increased to give a temperature of 540°C (1000°F) in the bed. These conditions are held for 2 hours. The bed is then cooled in air to 204°C (400°F), then in N₂ to less than 53°C (125°F) and sampled.

[0066] At this point a second batch of impregnated catalyst is made. The first batch of 1090 kg (2,400 lbs) is discharged from the ion exchange/calcination vessel. The remaining dried extrudate is loaded into the vessel, and the foregoing impregnation procedure is repeated exactly. The two batches are then combined in the vessel for one final impregnation.

[0067] The final impregnation step, draining, drying and calcination are exactly as hereinbefroe described except that the vessel contains about 2180 kg (4,800 Ibs) of extrudate. Magnesium nitrate solution is reused from the solution tank. Intermediate samples and final products have the following characteristics.

Example XI

[0068] The catalyst samples from the foregoing examples are tested for their ability to promote alkylation of toluene with ethylene. In the procedure for conducting such testing, approximately 15 cm³ of catalyst are charged to a 16 mm (J") diameter stainless steel reactor fitted with a central thermowell. The reactor is placed in a three zone split furnace and heated in flowing N₂ to 427°C (800°F). N₂ is then replaced by H₂, toluene is introduced, followed by ethylene. The inlet temperature to the reactor is adjusted to 432°C (810°F). The pressure is controlled at 791 kPa (100 psig) inlet to the reactor, and the flows are adjusted to give an 8.8:1.3 molar ratio of toluene/ethylene/hydrogen. On a WHSV basis, this is 29:1:0.2 (i.e. 29 g toluene/g catalyst/hour).

[0069] Two hours after introduction of ethylene (line-out period), collection of the liquid product is begun. After one hour, the product is removed, weighed and analyzed by gas chromatograph. Gas produced during the hour is also measured volumetrically and analyzed by mass spectroscopy.

[0070] Data from these analyses are combined by computer program to give an overall material-balanced run result. Especially noted is the proportion of para-ethyltoluene in ethyltoluenes, PET/ET, and the ratio of toluene converted to theoretical toluene conversion if all ethylene fed reacted stoichiometrically with toluene to give ethyltoluene.

[0071] Results for such testing of catalyst samples from Examples I-X are set forth in Table I.

Claims

1. A method for making a magnesium-containing zeolite-based alkylation catalyst composition suitable to promote the alkylation of mono-substituted aromatic compounds to a disubstituted aromatic product enriched in the 1, 4-isomer, the method comprising the steps of preparing a base catalyst comprising a siliceous crystalline zeolite material having a silica to alumina molar ratio of at least 12 and a Constraint Index in the range 1 to 12, contacting said base catalyst with an aqueous solution of magnesium nitrate so as to incorporate magnesium nitrate with said base catalyst, and calcining said magnesium nitrate-treated catalyst; characterized in that

a) the zeolite material of said base catalyst has a crystal major dimension of 1 to 10 _Ilm and a crystal minor dimension of 0.4 to 4 pm and comprises 1 % to 99% by weight of the base catalyst, the base catalyst also comprising from 1 % to 99% by weight of an inorganic oxide binder;

b) the contacting with said magnesium nitrate solution occurs without either prior or subsequent contact of the base catalyst with a solution of a phosphorus compound and is arranged so that after said calcination step, the catalyst contains from 4% to 8% of magnesium, present at least in part as magnesium oxide, by weight of the base catalyst;

c) the calcination step is performed in a nitrogen- or oxygen-containing atmosphere at a temperature of 200°C to 565°C; and

d) the final alkylation catalyst is substantially free of phosphorus.

2. A method according to Claim 1 wherein said contacting of base catalyst composite occurs in a single stage operation without intermediate calcination of said composite.

3. A method according to Claim 1 or 2 wherein said siliceous crystalline zeolite is selected from ZSM-5, ZSM-11, ZSM-12, SZM-23, ZSM-35, ZSM-38 or ZSM-48.

4. A method according to any of Claims 1 to 3 wherein said zeolite crystal major dimension ranges from 2 to 4 pm and said zeolite crystal minor dimension ranges from 0.5 to 2 pm.

5. A method according to any of Claims 1 to 4 wherein said aqueous solution of magnesium nitrate used to contact said base catalyst composite comprises Mg(NO₃)₂.6H₂O present to the extent of from 40% to 65% by weight of solution.

6. A phosphorus-free, magnesium-containing, zeolite-based, aromatics alkylation catalyst composition prepared in accordance with the method of any of Claims 1 to 5.

7. A base catalyst suitable for providing, upon calcination, an aromatics alkylation catalyst comprising a crystalline zeolite material having a silica to alumina molar ratio of at least 12 and a Constant Index within the range 1 to 12, and magnesium nitrate incorporated with the base catalyst, characterized in that the zeolite material has a crystal major dimension of 1 to 10 Ilm and a crystal minor dimension of 0.2 to 4 pm and comprises 1% to 99% by weight of the base catalyst, the base catalyst further comprising 1% to 99% by weight of an inorganic oxide binder, the magnesium nitrate is incorporated with the base catalyst such that the calcined alkylation catalyst comprises 4% to 8% by weight of magnesium, and the alkylation catalyst is free of phosphorus.

8. A modified base catalyst composite according to Claim 7 wherein said siliceous crystalline zeolite material is ZSM-5.

9. A modified base catalyst-composite according to Claim 8 wherein said ZSM-5 zeolite comprises from 25% to 80% by weight of said composite which also contains an alumina binder.

10. A process for the alkylation of a monoalkyl-substituted aromatic compound to produce a mixture of dialkyl-substituted aromatic compounds enriched in the 1, 4-isomer, said process comprising contacting the monoalkyl-substituted aromatic compound with an alkylating agent in the presence of a phosphorus-free, magnesium-containing zeolite based alkylation catalyst prepared by the method of any one of Claims 1 to 6 or prepared by calcination of the base catalyst of Claim 7.

11. An alkylation process according to Claim 10 wherein said alkylation conditions include a reaction temperature of between 300°C and 650°C, a molar ratio of alkylating agent to aromatic compound of from 0.05 to 2 and a weight hourly space velocity of reactant feed of from 1 to 50.

12. An alkylation process according to Claim 10 or Claim 11 wherein said aromatic compound is selected from toluene and ethylbenzene and said alkylating agent contains from 1 to about 16 carbon atoms and is selected from olefins, alkyl halides and alkanols.

13. An alkylation process according to any of Claims 10 to 12 wherein said aromatic compound is toluene and said alkylating agent is ethylene.

14. An alkylation process according to any of Claims 10 to 13 wherein said siliceous crystalline zeolite material is ZSM-5.

Ansprüche

1. Verfahren zur Herstellung einer Magnesium enthaltenden auf Zeolith basierenden Alkylierungskatalysator-Zusammensetzung, die geeignet ist, die Alkylierung, von monosubstituierten aromatischen Verbindungen zu einem disubstituierten aromatischen Produkt zu fördern, das mit dem 1,4-lsomer angereichert ist, wobei das Verfahren die Stufen umfaßt: Herstellung eines Grundkatalysators, der ein siliziumdioxidhaltiges kristallines Zeolithmaterial mit einem Siliziumdioxid/Aluminiumoxid-Molverhältnis von mindestens 12 und einem Zwangsindex im Bereich von 1 bis 12 umfaßt, Inkontaktbringen des Grundkatalysators mit einer wässrigen Lösung von Magnesiumnitrat, um das Magnesiumnitrat in den Grundkatalysator einzuarbeiten, und Calcinierung des mit Magnesiumnitrat behandelten Katalysators, dadurch gekennzeichnet, daß

a) das Zeolithmaterial des Grundkatalysators eine Kristallaußenabmessung von 1 bis 10 µm und eine Kristallinnenabmessung von 0,4 bis 4 um hat und 1 bis 99 Gew.-% des Katalysators umfaßt, wobei der Grundkatalysator ebenfalls von 1 bis 99 Gewe.-% eines Bindemittels eines anorganischen Oxids umfaßt,

b) das Inkontaktbringen mit der Magnesiumnitratlösung ohne entweder vorherigem oder nachfolgendem Kontakt des Grundkatalysators mit einer Lösung einer Phosphorverbindung auftritt und so angeordnet ist, daß nach der Calcinierungsstufe der Katalysator von 4 bis 8% Magnesium enthält, das zumindest teilweise als Magnesiumoxid vorhanden ist, bezogen auf das Gewicht des Grundkatalysators,

c) die Calcinierungsstufe in einer Stickstoff oder Sauerstoff enthaltenden Atmosphäre bei einer Temperatur von 200 bis 565°C durchgeführt wird und

d) der Alkylierungs-Endkatalysator im wesentlichen frei von Phosphor ist.

2. Verfahren nach Anspruch 1, worin das Inkontaktbringen der Grundkatalysator-Zusammensetzung in einem Einzelstufen-Verfahren ohne Zwischencalcinierung der Zusammensetzung erfolgt.

3. Verfahren nach Anspruch 1 oder 2, worin der siliziumdioxidhaltige kristalline Zeolith aus ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38 oder ZSM-48 ausgewählt ist.

4. Verfahren nach einem der Ansprüche 1 bis 3, worin die Kristallaußenabmessung des Zeoliths im Bereich von 2 bis 4 um und die Kristallinnenabmessung des Zeoliths im Bereich von 0,5 bis 2 µm liegen.

5. Verfahren nach einem der Ansprüche 1 bis 4, worin die wässrige Lösung von Magnesiumnitrat, die zum Kontakt der Grundkatalysator-Zusammensetzung verwendent wird, Mg(NO₃)₂.6H₂O bis zum Ausmaß von 40 bis 65 Gew.-% der Lösung umfaßt.

6. Phosphorfreie, Magensium enthaltende, auf Zeolith basierende Alkylierungskatalysator-Zusammensetzung für Aromaten, hergestellt entsprechend dem Verfahren nach einem der Ansprüche 1 bis 5.

7. Grundkatalysator, nach der Calcinierung zur Schaffung eines Alkylierungskatalysators für Aromaten geeignet, welcher ein kristallines Zeolithmaterial mit einem Siliziumdioxid/Aluminiumoxid-Molverhältnis von mindestens 12 und einem Zwangsindex innerhalb des Bereiches von 1 bis 12 und ein in den Grundkatalysator eingearbeitetes Magnesiumnitrat umfaßt, dadurch gekennzeichnet, daß das Zeolithmaterial eine Kristallaußenabmessung von 1 bis 10 pm und eine Kristallinnenabmessung von 0,2 bis um hat und 1 bis 99 Gew.-% des Grundkatalysators umfaßt, wobei der Grundkatalysator weiterhin 1 bis 99 Gew.-% eines Bindemittels eines anorganischen Oxids umfaßt, das Magnesiumnitrat in den Grundkatalysator eingearbeitet ist, so daß der calcinierte Akylierungskatalysator 4 bis 8 Gew.-% Magnesium umfaßt und der Alkylierungskatalysator frei von Phosphor ist.

8. Modifizierte Grundkatalysator-Zusammensetzung nach Anspruch 7, worin das siliziumdioxidhaltige kristalline Zeolithmaterial ZSM-5 ist.

9. Modifizierte Grundkatalysator-Zusammensetzung nach Anspruch 8, worin der Zeolith ZSM-5 von 25 bis 80 Gew.-% der Zusammensetzung umfaßt, die ebenfalls ein Aluminiumoxid-Bindemittel enthält.

10. Verfahren zur Alkylierung einer monoalkylsubstituierten aromatischen Verbindung, um eine Mischung von dialkylsubstituierten aromatischen Verbindungen herzustellen, die mit dem 1,4-lsomer angereichert sind, wobei bei dem Verfahren die monoalkylsubstituierte aromatische Verbindung mit einem Alkylierungsmittel in Gegenwart eines phosphorfreien, Magnesium enthaltenden auf Zeolith basierenden Alkylierungskatalysator in Kontakt gebracht wird, der entsprechend dem Verfahren nach einem der Ansprüche 1 bis 6 hergestellt wurde, oder durch Calcinierung des Grundkatalysators nach Anspruch 7 hergestellt wurde.

11. Alkylierungsverfahren nach Anspruch 10, worin die Alkylierungsbedingungen eine Reaktionstemperatur von zwischen 300 und 650°C, ein Molverhältnis des Alkylierungsmittel zur aromatischen Verbindung von 0,05 bis 2 und eine stündliche Gewichts-Raum-Geschwindigkeit der Reaktantenzufuhr von 1 bis 50 umfassen.

12. Alkylierungsverfahren nach Anspruch 10 oder 11, worin die aromatische Verbindung aus Toluol und Äthylbenzol ausgewählt ist und das Alkylierungsmittel von 1 bis etwa 16 Kohlenstoffatomen enthält und aus Olefinen, Alkylhalogeniden und Alkanolen ausgewählt ist.

13. Alkylierungsverfahren nach einem der Ansprüche 10 bis 12, worin die aromatische Verbindung Toluol ist und das Alkylierungsmittel Äthylen ist.

14. Alkylierungsverfahren nach einem der Ansprüche 10 bis 13, worin das siliziumdioxidhaltige kristalline Zeolith-Material ZSM-5 ist.

Revendications

1. Procédé pour préparer une composition de catalyseur d'alkylation à base de zéolite contenant du magnésium, convenant pour favoriser l'alkylation de composés aromatiques monosubstitués en un produit aromatique disubstitué enrichi en isomère 1,4, le procédé contenant les étapes consistant à préparer un catalyseur de base comprenant une matière zéolitique cristalline siliceuse ayant un rapport molaire de la. silice à l'alumine au moins égal à 12 et un indice de contrainte compris entre 1 et 12, à mettre ce catalyseur de base en contact avec une solution aqueuse de nitrate de magnésium de façon à incorporer le nitrate de magnésium dans ce catalyseur de base, et à calciner ledit catalyseur traité par du nitrate de magnésium, procédé caractérisé en ce que:

a) la matière zéolitique dudit catalyseur de base présente une dimension majeure de cristal de 1 à 10 pm et un dimension mineure de cristal de 0,4 à 4 pm et comprend 1 % à 99% en poids du catalyseur de base, le catalyseur de base comprenant aussi de 1 % à 99% en poids d'un liant du type oxyde minéral;

b) la mise en contact avec ladite solution de nitrate de magnésium s'effectue sans contact, préalable ou subséquent, du catalyseur de base avec une solution d'un composé du phosphore et elle est agencée de manière que, après ladite étape de calcination, le catalyseur contienne de 4% à 8% de magnésium, présent au moins en partie sous forme d'oxyde de magnésium, en poids du catalyseur de base;

c) on effectue l'étape de calcination dans une atmosphère contenant de l'azote ou de l'oxygène à une température de 200°C à 565°C; et

d) le catalyseur final d'alkylation est essentiellement dépourvu de phosphore.

2. Procédé selon la revendication 1, dans lequel ladite mise en contact du composite de base pour catalyseur se produit en une opération en une seule étape sans calcination intermédiaire dudit composite.

3. procédé selon la revendication 1 ou 2, dans lequel ladite zéolite cristalline siliceuse est choisie parmi ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38 ou ZSM-48.

4. Procédé selon l'une quelconque des revendications 1 à 3, dans lequel ladite dimension majeure du cristal de zéolite se situe entre 2 et 4 pm et ladite dimension mineure du cristal de zéolite se situe entre 0,5 et 2 pm.

5. Procédé selon l'une quelconque des revendications 1 à 4, dans lequel ladite solution aqueuse de nitrate de magnésium que l'on utilise pour la mettre en contact avec ledit composite de base pour catalyseurs comprend Mg(NO₃)₂.6H₂O, présent à raison de 40% à 65% en poids de la solution.

6. Composition de catalyseur d'alkylation d'aromatiques, à base de zéolite, contenant du magnésium et dépourvue de phosphore, préparée selon la procédé selon l'une quelconque des revendications 1 à 5.

7. Catalyseur de base convenant pour fournir, après calcination, un catalyseur pour l'alkylation des aromatiques, comprenant une matière zéolitique cristalline ayant un rapport molaire de la silice à l'alumine au moins égal à 12 et un indice de contrainte compris entre 1 et 12, et du nitrate de magnésium incoporé au catalyseur de base, catalyseur caractérisé en ce que la matière catalytique possède une dimension majeure de cristal de 1 à 10 pm et une dimension minneure de cristal de 0,2 à 4 pm et comprend 1 % à 99% en poids du catalyseur de base, le catalyseur de base comprenant en outre 1 % à 99% en poids d'un liant de type oxyde minéral, le nitrate de magnéseium est incorporé au catalyseur de base de manière que le catalyseur d'alkylation, calciné, comprenne 4% à 8% en poids de magnésium, et le catalyseur d'alkylation est dépourvu de phosphore.

8. Composite de catalyseur de base modifié selon la revendication 7, dans lequel ladite matière zéolitique cristalline siliceuse est ZSM-5.

9. Composite de catalyseur de base modifié selon la revendication 8, dans lequel ladite zéolite ZSM-5 constitue de 25% à 80% du poids dudit composite, lequel contient également un liant à base d'alumine.

10. Procédé pour l'alkylation d'un composé monoalkylaromatique pour produire un mélange de composés dialkyl-aromatiques enrichis en l'isomère 1,4-, ce procédé comprennent la mise en contact du composé monoalkyl-aromatique avec un agent d'alkylation en présence d'un catalyseur d'alkylation à base de zéolite contenant du magnésium, sans phosphore, préparé par le procédé selon l'une quelconque des revendications 1 à 6 our préparé par calcination du catalyseur de base selon la revendication 7.

11. Procédé d'alkylation selon la revendication 10, dans lequel lesdites conditions d'alkylation comprennent une température de réaction comprise entre 300°C et 650°C, un rapport molaire de l'agent d'alkylation au composé aromatique allant de 0,05 à 2 et une vitesse spatiale horaire en poids de. l'alimentation à faire réagir allant de 1 à 50.

12. Procdédé d'alkylation selon la revendication 10 ou la revendication 11, dans lequel ledit comporé aromatique est choisi parmi le toluène et l'éthylbenzène, et ledit agent d'alkylation contient de I à environ 16 atomes de carbone et est choisi parmi de oléfines, des halogénures d'alkyle et des alcanols.

13. Procédé d'alkylation selon l'une quelconque des revendications 10 à 12, dans lequel ledit composé aromatique est le toluène et ledit agent d'alkylation est l'éthylène.

14. Procédé d'alkylation selon l'une quelconque des revendications 10 à 13, dans lequel ladite matière zéolitique cristalline siliceuse est ZSM-5.